EP2121551B1 - Glycerinverdampfungsverfahren - Google Patents

Glycerinverdampfungsverfahren Download PDF

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Publication number
EP2121551B1
EP2121551B1 EP08799845A EP08799845A EP2121551B1 EP 2121551 B1 EP2121551 B1 EP 2121551B1 EP 08799845 A EP08799845 A EP 08799845A EP 08799845 A EP08799845 A EP 08799845A EP 2121551 B1 EP2121551 B1 EP 2121551B1
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EP
European Patent Office
Prior art keywords
glycerol
fluidized bed
solid
inert solid
solution
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Not-in-force
Application number
EP08799845A
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English (en)
French (fr)
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EP2121551A1 (de
Inventor
Jean-Luc Dubois
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Arkema France SA
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Arkema France SA
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Publication date
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Priority to PL08799845T priority Critical patent/PL2121551T3/pl
Publication of EP2121551A1 publication Critical patent/EP2121551A1/de
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Publication of EP2121551B1 publication Critical patent/EP2121551B1/de
Not-in-force legal-status Critical Current
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0011—Heating features
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying
    • B01D1/18—Evaporating by spraying to obtain dry solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/18—Polyhydroxylic acyclic alcohols
    • C07C31/22—Trihydroxylic alcohols, e.g. glycerol
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/51—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition
    • C07C45/52—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition by dehydration and rearrangement involving two hydroxy groups in the same molecule
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C57/00—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms
    • C07C57/02—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms with only carbon-to-carbon double bonds as unsaturation
    • C07C57/03—Monocarboxylic acids
    • C07C57/04—Acrylic acid; Methacrylic acid

Definitions

  • the present invention relates to a method of vaporizing aqueous glycerol solutions in a fluidized bed containing an inert solid, for simultaneously removing impurities present in these solutions or generated during evaporation.
  • Glycerol is a chemical, 1,2,3-propane triol, which can be obtained either by chemical synthesis from propylene or as a co-product formed during the methanolysis of vegetable oils.
  • the methanolysis of vegetable oils can be carried out according to various processes, in particular by using homogeneous catalysis such as sodium hydroxide or sodium methylate dissolved in methanol, or by using heterogeneous catalysis.
  • homogeneous catalysis such as sodium hydroxide or sodium methylate dissolved in methanol
  • heterogeneous catalysis we can refer to this topic in the article D. Ballerini et al. in the chemical news of nov-dec 2002 .
  • Methyl esters are used in particular as fuels or fuels in diesel and heating oil.
  • VOMEs vegetable oil methyl esters
  • Glycerol from vegetable oils is a natural product of renewable origin and is thus increasingly available. In the current framework of new concept of green chemistry, and more generally of sustainable development, it becomes more and more interesting to value this product.
  • glycerol more or less pure and more or less diluted in water.
  • glycerine these more or less pure aqueous solutions of glycerol which are called glycerine, according to the definition adopted by the Soap and Detergent Association ( Soaps and Detergents: A Miami Beach Fla., Oct. 12-14, 1994, chapter 6 pp172-206. Ed: Spitz L, AOCS Press, Champaign ).
  • Crude glycerine generally has a composition of the order of 88% glycerol, 9-10% water and 2-3% impurities.
  • the glycerol may contain impurities such as basic salts (for example sodium or potassium), non-glycerinous organic compounds, methanol or residues of vegetable oils.
  • impurities such as basic salts (for example sodium or potassium), non-glycerinous organic compounds, methanol or residues of vegetable oils.
  • basic salts for example sodium or potassium
  • non-glycerinous organic compounds for example methanol or residues of vegetable oils.
  • methanol residues of vegetable oils.
  • impurities such as basic salts (for example sodium or potassium), non-glycerinous organic compounds, methanol or residues of vegetable oils.
  • the presence of these impurities is particularly detrimental for the reactions used or for the quality of the finished products.
  • sodium or potassium salts is detrimental to the catalytic dehydration reaction of glycerol to acrolein, since these salts are capable of poisoning the acid sites of the catalysts used. artwork.
  • aqueous solutions of crude glycerol or glycerin generally require prior treatment before use, or purification treatment to consider new applications.
  • the treatments of crude solutions of glycerol proposed aim at the elimination of the dissolved salts and the organic impurities resulting from the bodies fat, the elimination of color, an increase in glycerol content, or the vaporization of glycerol, depending on the intended final application.
  • evaporation, distillation, lime treatment (to neutralize residual fatty acids) followed by filtration, ion exchange or ionic exclusion treatment, osmosis separation can be carried out. reverse or electrodialysis.
  • multi-effect evaporators are used to concentrate dilute glycerol solutions.
  • a triple effect evaporator it is possible to evaporate 2.4 kg of water with 1 kg of steam.
  • Distillation is one of the techniques used to concentrate and purify glycerine. As glycerol begins to decompose at about 202 ° C, well below its boiling point (293 ° C), it is necessary to distil the glycerin in several stages using a reduced pressure. In some cases distillation is done by batch operations until salts and non-volatile compounds have accumulated sufficiently in the capacity. The operation is then stopped and the capacity discharged from the impurities before restarting the distillation. The evaporation is carried out under vacuum, and the partial condensation of glycerol (which will condense before the water) at the outlet of the unit makes it possible to directly obtain a concentrated glycerol. Typically, pressures of 10 mmHg are used, for a temperature of 160-165 ° C, which gives low partial pressures of glycerol in the vapor phase.
  • Distilled glycerin still contains colored compounds. It is sometimes necessary to bleach glycerine for pharmaceutical and food applications. Typically activated charcoal is added to the glycerin to discolor it.
  • Glycerin purification by ion exclusion has also been developed and uses ionic resins to separate soluble ionic salts in aqueous solution from nonionic compounds such as glycerol. It is a technique that avoids the consumption of heat and chemical regenerants, and allows to purify highly contaminated streams like raw glycerin, using only water as a chemical regenerant.
  • Aqueous solutions of glycerol which are weakly contaminated with salts can be exchanged simply on acidic and basic resins.
  • the glycerol solutions thus purified can then be concentrated by evaporation.
  • Glycerine and sodium hydroxide solutions obtained after transesterification of rapeseed oil were demineralized by membrane electrodialysis to produce pure glycerine. This technique is described in the reference: Schaffner, F. et al. Proc. - World Filtr. Cong. 7th, Volume 2, 629-633 .
  • temperature control is very critical because certain undesirable reactions can take place, such as the formation of nitrogen compounds by degradation of proteinaceous material present in glycerin, the formation of ester volatile glycerine by reaction with low molecular weight soaps, polyglycerol formation, acrolein formation which contributes to the smells of the final product. It is therefore important to limit the residence time of glycerin at high temperature, as well as this temperature.
  • the evaporation processes used conventionally do not allow to have high partial pressures of glycerol in the vapor phase.
  • TUICHIEV discloses a method for purifying glycerol in a fluidized bed containing an ion exchange resin.
  • the Applicant Company has now surprisingly discovered a one-step process for vaporizing an aqueous solution of glycerol and simultaneously removing impurities present or generated during evaporation in this solution.
  • the subject of the present invention is therefore a process for vaporizing aqueous solutions of glycerol (or glycerine) in a fluidized bed containing an inert solid.
  • the aqueous solution is injected directly into a fluidized bed containing an inert solid maintained at a temperature sufficient to allow instantaneous vaporization of glycerol and water.
  • inert solids it is possible to use, for example, sand, glass or quartz powder, silicon carbide, or solids with a low specific surface area, the low surface area solids being inherently inert, they can be composed of of alumina, silica or silica-alumina. It is not within the scope of the invention using as inert solid a mineral salt, such as sodium chloride (NaCl), potassium chloride (KCl), sodium sulphate (Na 2 SO 4 ) or sulphate potassium (K 2 SO 4 ).
  • the inert solid is selected from sand, silica, quartz and silicon carbide.
  • the fluidization can be ensured by the vaporization of the glycerol solution, and / or by a stream of inert gas (nitrogen, CO 2 , recycle gas, etc.), or of air, of oxygen, or of a gas mixture.
  • inert gas nitrogen, CO 2 , recycle gas, etc.
  • the temperature of the fluidized bed is generally between 220 and 350 ° C, preferably 260 to 320 ° C.
  • the process according to the invention leads to high partial pressures of glycerol in the vapor phase, which has the advantage of vaporizing glycerol with a much higher productivity than that obtained with vacuum distillation.
  • the impurities present in the aqueous solution are eliminated simultaneously, because the fluidized bed technique allows a part of the solid to be withdrawn continuously to regenerate it ex situ.
  • the organic compounds present in the glycerol solution but also the products resulting from the decomposition of glycerol during this evaporation step can lead to the formation of coke which is deposited on the inert solid.
  • the aqueous solution of glycerol contains salts (for example sodium chloride, or sodium sulphate), these salts are also deposited on the inert solid during the evaporation of the aqueous glycerol solution.
  • the inert solid comprising coke and / or mineral salts can then be withdrawn continuously to be regenerated in another reactor, before being returned to the fluidized bed.
  • the removal of mineral salts can be carried out by simple washing with water of the solid, or any other appropriate technique.
  • Regeneration of the solid consists of a combustion of solid deposits, it is generally carried out with air in a reactor which may be for example another continuously operated fluidized bed, a fixed bed, or any other reactor that may be suitable.
  • a fluidized bed operated continuously will be used.
  • the combustion of the carbonaceous deposits on the inert solid not only makes it possible to regenerate it but also to heat it up before returning it to the glycerol evaporation fluidized bed. This combustion can be carried out in the presence of a fuel, for example methane, which contributes to bringing the inert solid to the temperature necessary for the evaporation of the aqueous glycerol solution.
  • the particles are moving relative to each other which causes an attrition of the solid.
  • this attrition which consumes solid and produces fine particles.
  • the attrition makes it possible to eliminate a part of the deposits which form on the inert solid.
  • the fine particles thus formed by attrition are removed downstream, for example by separation in a cyclone or by filtration.
  • an aqueous solution of glycerol or glycerin (4) is introduced into a reactor (1) containing a fluidized bed of an inert solid.
  • the fluidization can optionally be ensured by a stream of inert gas (nitrogen, CO 2 , recycle gas, etc.), or air, oxygen, or a mixture of gases that can be chosen so that the composition at 8 corresponds best to the feed of the processes downstream.
  • the fluidized bed is heated via the heat exchanger (3).
  • Glycerol vapors and water are extracted from the reactor (8) and a unit (7) can recover the fine particles of the installation.
  • a unit (6) is used to wash the solid used in the fluidized bed to remove deposited mineral salts.
  • the reactor (2) is a regenerator of the inert solid in which the solid withdrawn from (1) is subjected to combustion in the presence of regeneration gas (5) containing molecular oxygen and / or fuels, the regenerated solid being returned to the reactor (1).
  • the gases from the regeneration unit are discharged at (9).
  • the glycerol vapors obtained according to this process are then directly usable in a downstream process using glycerol in gas form, such as, for example, the processes for producing acrolein or acrylic acid described in the documents WO 06/087083 , WO 06/087084 , WO 06/114506 , WO 07/090990 and WO 07/090991 , or a process for producing acrylonitrile as described in the application FR07.53293 . They can also be condensed to produce concentrated and purified aqueous glycerol solutions.
  • the invention also relates to the use of a fluidized bed containing an inert solid for vaporizing and purifying aqueous solutions of glycerol.
  • the fluidized bed consists of a stainless steel tube 41 mm in diameter and a total height of 790 mm.
  • the fluidized bed is immersed in a fluidized sand bath, heated by electric elements installed inside the bath. Three thermocouples recorded the temperature gradient along the tube. Air was supplied at a rate of 500 ml / min (normal conditions) below a porous metal plate which distributes gas through the reactor diameter.
  • the test solution / nitrogen mixture is fed by a metal tube of 0.6 mm which goes to the bottom of the bed with a mass flow rate of 0.5 g / min, maintaining the nitrogen flow rate at 1000 ml / min. .
  • the total pressure in the fluidized bed is 1.2 bar and the temperature is maintained at 310 ° C.
  • the experiment was carried out with an aqueous solution containing 18% by weight of pure glycerol (99.5% LAB MAT) and 2% by weight of NaCl salt for 60 min, which corresponds to a total mass of 0.6 g salt fed to the inlet of the fluidized bed.
  • the products are collected at the outlet of the fluidized bed and condensed to be analyzed by conductivity.
  • the total salt mass recovered in the condenser is 0.0004 g, which corresponds to an efficiency of 99.9% for the separation of salt on the fluidized bed, reflected by the low conductivity of the solution collected in the condenser.

Claims (4)

  1. Verfahren, bei dem wässerige Lösungen von Glycerol in einer Wirbelschicht verdampft werden, die einen inerten Feststoff enthält und auf einer Temperatur im Bereich von 220 bis 350 °C gehalten wird.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass es sich bei dem inerten Feststoff um Stand, Glaspulver oder Quarzpulver, Siliciumcarbid oder um eignen Feststoff mit kleiner spezifischer Oberfläche handelt.
  3. Verfahren mach Anspruch 1 oder 2, dadurch gekennzeichnet, dass der Feststoff in einer zweiten Wirbelschicht regeneriert wird, die kontinuierlich betrieben wird.
  4. Verwendung einer Wirbelschicht, die einen inerten feststoff enthält, zum Verdampfern und zum Reinigen von wässerigen Lösungen von Glycerol.
EP08799845A 2007-03-19 2008-03-14 Glycerinverdampfungsverfahren Not-in-force EP2121551B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL08799845T PL2121551T3 (pl) 2007-03-19 2008-03-14 Sposób odparowywania glicerolu

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0753896A FR2913974A1 (fr) 2007-03-19 2007-03-19 Procede de vaporisation de glycerol
PCT/FR2008/050438 WO2008129208A1 (fr) 2007-03-19 2008-03-14 Procede de vaporisation de glycerol

Publications (2)

Publication Number Publication Date
EP2121551A1 EP2121551A1 (de) 2009-11-25
EP2121551B1 true EP2121551B1 (de) 2010-08-04

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ID=38657143

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08799845A Not-in-force EP2121551B1 (de) 2007-03-19 2008-03-14 Glycerinverdampfungsverfahren

Country Status (15)

Country Link
US (1) US8148582B2 (de)
EP (1) EP2121551B1 (de)
JP (1) JP5270586B2 (de)
KR (1) KR101516831B1 (de)
CN (1) CN101687743B (de)
AT (1) ATE476405T1 (de)
BR (1) BRPI0808967A2 (de)
DE (1) DE602008002059D1 (de)
DK (1) DK2121551T3 (de)
ES (1) ES2349395T3 (de)
FR (1) FR2913974A1 (de)
MY (1) MY148567A (de)
PL (1) PL2121551T3 (de)
PT (1) PT2121551E (de)
WO (1) WO2008129208A1 (de)

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2920767B1 (fr) * 2007-09-06 2009-12-18 Arkema France Procede de vaporisation reactive de glycerol
FR2925490B1 (fr) 2007-12-20 2009-12-25 Arkema France Procede de synthese d'acroleine a partir de glycerol
FR2948366B1 (fr) 2009-07-22 2012-08-17 Arkema France Procede de fabrication d'acide acrylique bio-ressource a partir de glycerol
FR2952056B1 (fr) 2009-11-04 2013-01-25 Arkema France Glutaraldehyde bioressource et ses procedes de fabrication
FR2952057B1 (fr) 2009-11-04 2011-11-18 Arkema France Procede de synthese de pyridine et picolines bioressourcees
JP5532842B2 (ja) * 2009-11-17 2014-06-25 株式会社Ｉｈｉ グリセリン改質装置及びグリセリン改質方法
JP5556152B2 (ja) * 2009-12-01 2014-07-23 株式会社Ｉｈｉ グリセリン精製装置及び精製方法並びにグリセリン改質装置及び改質方法
FR2954311B1 (fr) 2009-12-22 2012-02-03 Arkema France Procede de synthese perfectionne d'acroleine a partir de glycerol
DE102010061814A1 (de) * 2010-11-23 2012-05-24 Wacker Chemie Ag Verfahren zum Aufarbeiten von flüssigen Rückständen der Direktsynthese von Organochlorsilanen
US20140165929A1 (en) * 2012-12-17 2014-06-19 Conocophillips Company Water with solvent indirect boiling
CN104707353A (zh) * 2015-02-12 2015-06-17 浙江华诺化工有限公司 甘油蒸馏系统
US10138139B2 (en) 2016-02-12 2018-11-27 Babcock Power Environmental Inc. Wastewater treatment systems and methods
CN107021871A (zh) * 2017-05-05 2017-08-08 中国科学院青岛生物能源与过程研究所 一种生物柴油副产粗甘油的纯化方法及其装置
CN110448927A (zh) * 2019-07-15 2019-11-15 天津大学 一种硫酸钠溶液循环流化床蒸发装置及其操作方法

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JPS62273027A (ja) * 1986-05-22 1987-11-27 Kubota Ltd ガス分離方法
JPH01250331A (ja) * 1988-03-31 1989-10-05 Nippon Oil & Fats Co Ltd グリセリンの精製法
JP3254752B2 (ja) * 1991-11-27 2002-02-12 住友化学工業株式会社 ε−カプロラクタムの製法
DE4238493C1 (de) * 1992-11-14 1994-04-21 Degussa Verfahren zur Herstellung von Acrolein und dessen Verwendung
RU2093503C1 (ru) * 1995-07-13 1997-10-20 Акционерное общество закрытого типа "Невская косметика" Способ дистилляции технического глицерина
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FR2882052B1 (fr) * 2005-02-15 2007-03-23 Arkema Sa Procede de deshydratation du glycerol en acroleine
FR2882053B1 (fr) 2005-02-15 2007-03-23 Arkema Sa Procede de deshydratation du glycerol en acrolene
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FR2897058B1 (fr) 2006-02-07 2008-04-18 Arkema Sa Procede de preparation d'acroleine

Also Published As

Publication number Publication date
KR20090121345A (ko) 2009-11-25
MY148567A (en) 2013-04-30
US8148582B2 (en) 2012-04-03
PT2121551E (pt) 2010-10-11
BRPI0808967A2 (pt) 2014-08-26
ES2349395T3 (es) 2010-12-30
CN101687743A (zh) 2010-03-31
EP2121551A1 (de) 2009-11-25
US20100230635A1 (en) 2010-09-16
DK2121551T3 (da) 2010-11-08
ATE476405T1 (de) 2010-08-15
KR101516831B1 (ko) 2015-05-04
FR2913974A1 (fr) 2008-09-26
JP2010522148A (ja) 2010-07-01
JP5270586B2 (ja) 2013-08-21
PL2121551T3 (pl) 2011-02-28
CN101687743B (zh) 2014-07-16
DE602008002059D1 (en) 2010-09-16
WO2008129208A1 (fr) 2008-10-30

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